US5179178A - Olefin polymerization - Google Patents

Olefin polymerization Download PDF

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Publication number
US5179178A
US5179178A US07/883,602 US88360292A US5179178A US 5179178 A US5179178 A US 5179178A US 88360292 A US88360292 A US 88360292A US 5179178 A US5179178 A US 5179178A
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US
United States
Prior art keywords
catalyst
process according
refractory oxide
oxide powder
range
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
US07/883,602
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English (en)
Inventor
Elizabeth M. Stacy
M. Bruce Welch
Shirley J. Martin
Max P. McDaniel
Dale E. Pierce
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Phillips Petroleum Co
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Phillips Petroleum Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to US07/883,602 priority Critical patent/US5179178A/en
Assigned to PHILLIPS PETROLEUM COMPANY A CORP. OF DELAWARE reassignment PHILLIPS PETROLEUM COMPANY A CORP. OF DELAWARE ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: MC DANIEL, MAX P., MARTIN, SHIRLEY J., WELCH, M. BRUCE, PIERCE, DALE E., STACY, ELIZABETH M.
Application filed by Phillips Petroleum Co filed Critical Phillips Petroleum Co
Publication of US5179178A publication Critical patent/US5179178A/en
Application granted granted Critical
Priority to CA002093461A priority patent/CA2093461C/en
Priority to AU36745/93A priority patent/AU651273B2/en
Priority to ZA932856A priority patent/ZA932856B/xx
Priority to KR1019930008053A priority patent/KR100278081B1/ko
Priority to JP11069493A priority patent/JP3268884B2/ja
Priority to MX9302763A priority patent/MX9302763A/es
Priority to NO931749A priority patent/NO300694B1/no
Priority to HU9301392A priority patent/HU211449B/hu
Priority to YU33293A priority patent/YU48361B/sh
Priority to AT93107880T priority patent/ATE146802T1/de
Priority to EP93107880A priority patent/EP0570000B1/en
Priority to DK93107880.2T priority patent/DK0570000T3/da
Priority to ES93107880T priority patent/ES2096138T3/es
Priority to SG1996005323A priority patent/SG43200A1/en
Priority to DE69306852T priority patent/DE69306852T2/de
Priority to GR960403669T priority patent/GR3022341T3/el
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

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Classifications

    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/02Ethene
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00Polymerisation catalysts
    • C08F4/42Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62Refractory metals or compounds thereof
    • C08F4/622Component covered by group C08F4/62 with an organo-aluminium compound
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00Polymerisation catalysts
    • C08F4/42Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62Refractory metals or compounds thereof
    • C08F4/63Pretreating the metal or compound covered by group C08F4/62 before the final contacting with the metal or compound covered by group C08F4/44
    • C08F4/632Pretreating with metals or metal-containing compounds
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S526/00Synthetic resins or natural rubbers -- part of the class 520 series
    • Y10S526/904Monomer polymerized in presence of transition metal containing catalyst at least part of which is supported on a polymer, e.g. prepolymerized catalysts

Definitions

  • the present invention relates to the polymerization of olefins.
  • the present invention relates to slurry or particle form polymerization.
  • the present invention relates to olefin polymerization using a continuous loop-type reactor.
  • the present invention relates to a novel method for charging prepolymerized polymerization catalyst to the polymerization zone.
  • a number of the later generation high activity olefin polymerization catalysts are prepared by processes which result in extremely fine catalyst particles.
  • the use of such fine catalyst particles in actual commercial polymerization has often led to various problems including the production of undesirable levels of fine polymer and undesired difficulties in handling the catalyst.
  • prepolymer on the catalyst introduces its own separate problems. For example, it has been noted that the presence of the prepolymer can result in plugged feeding lines and feeding difficulties in mud pots which arise from the tendency of such prepolymerized catalysts to bridge in the restrictive openings of either mud pots or feed lines. These problems become particularly evident as the level of prepolymer on the catalyst is increased.
  • the feeding of catalyst slurries can even be a problem for particulate olefin polymerization catalysts that have not been subjected to prepolymerization, for example particulate chromium-containing catalysts.
  • An object of the present invention is to provide an improved method for charging a slurry of particulate olefin polymerization catalyst to the reaction zone.
  • Another object of the present invention is to provide a process for polymerizing olefins with a particulate olefin polymerization catalyst and a particulate diluent which has a less adverse effect upon the properties of the ultimate polymer than diluents heretofore used.
  • Another object of the present invention is to provide a process for polymerizing olefins which allows one to use olefin polymerization catalysts containing much higher levels of prepolymer than have generally been used in the past.
  • a process for polymerizing olefins comprising charging a liquid slurry of particulate olefin polymerization catalyst through a restrictive opening into a polymerization zone wherein said catalyst is contacted with at least one olefin under suitable polymerization conditions, wherein said slurry of prepolymerized olefin polymerization catalyst has been prepared by combining a refractory oxide powder with a suitable liquid and said particulate catalyst, said refractory oxide powder being selected from the group consisting of fumed silica, fumed titanium dioxide, and fumed alumina and being added to the slurry in an amount sufficient to improve the flow of the catalyst through the restrictive opening.
  • the present invention is considered to be particularly applicable for processes employing olefin polymerization catalysts of the type disclosed in U.S. Pat. No. 4,325,837, the disclosure of which is incorporated herein by reference.
  • An especially preferred type of olefin polymerization catalyst is prepared by contacting magnesium dichloride and a titanium alkoxide in a liquid to obtain a solution, then contacting the solution with an alkylaluminum halide to obtain a solid, then contacting the solid with an olefin to obtain a prepolymerized solid and then contacting the resulting prepolymerized solid with titanium tetrachloride.
  • the titanium alkoxide is a titanium tetrahydrocarbyl oxide of the formula Ti(OR) 4 wherein each R is individually selected from an alkyl group containing from about 1 to about 10 carbon atoms, more preferably about 1 to about 4 carbon atoms. It is also currently preferred to employ as the precipitating agent an alkylaluminum halide of the formula R m AlZ 3-m wherein R is a alkyl group having 1 to 8 carbon atoms, Z is a halogen, hydrogen, or hydrocarbyl group having 1 to 8 carbons and m is a number in the range of 1 to 3.
  • Such prepolymerized catalyst can have the prepolymer deposited thereon by prepolymerization such as taught in the aforementioned U.S. Pat. No. 4,325,837. It is also within the scope of the present invention to have the prepolymer deposited upon the catalyst by various other means such as plasma or flame spraying of a polymer coating, or the slurrying of the catalyst with a polymer solution followed by the addition of a countersolvent to precipitate the polymer.
  • the currently preferred process involves prepolymerizing and then treating the resulting catalyst with titanium tetrachloride. In an especially preferred embodiment the resulting titanium tetrachloride-treated catalyst is then contacted with a organometallic reducing agent before the catalyst is introduced into the polymerization zone.
  • the solid is washed with a hydrocarbon after the treatment with the organometallic compound.
  • This pretreatment of the catalyst with the reducing agent has been found to reduce the tendency of the catalyst to cause reactor fouling during polymerization.
  • the currently preferred organometallic reducing agents are those of the formula R m AlZ 3-m wherein R is a hydrocarbyl group having 1 to 8 carbons, Z is a halogen, hydrogen, or hydrocarbyl group having 1 to 8 carbons, and m is a number in the range of 1 to 3.
  • the currently most preferred reducing agents for this step are triethylaluminum and diethylaluminum chloride.
  • the weight percent of prepolymer can vary over a wide range, typically in the range of about 1 to about 95 weight percent, more generally in the range of about 1 to about 80 weight percent, and still more preferably in the range of about 1 to about 50 weight percent.
  • the particulate catalyst is combined with a suitable amount of the refractory oxide powder.
  • suitable refractory oxide powders include the fumed, or pyrogenic, silicas, aluminas, and titanium dioxides.
  • the currently preferred refractory oxide is fumed silica. Most typically the refractory oxide that is employed would have an average primary particle size in the range of about 0.001 micron to about 0.1 micron, more preferably about 0.001 micron to about 0.03 micron.
  • the currently preferred fumed silica has an average primary particle size in the range of about 0.005 to about 0.02 microns, still more preferably about 0.005 to about 0.015 microns.
  • the catalyst and the refractory oxide powder are combined in a liquid.
  • a liquid that is suitable for use in the olefin polymerization can be employed.
  • substantially dry, i.e. anydrous, organic liquids can be employed.
  • Some typical examples include dichloromethane, hexane, heptane, isobutane, cyclohexane, and the like.
  • the weight ratio of the fumed silica to the solid catalyst is preferred for the weight ratio of the fumed silica to the solid catalyst to be in the range of about 0.05/1 to about 0.30/1, still more preferably about 0.12/1 to about 0.25/1.
  • the slurry of the catalyst and the refractory oxide powder is employed in polymerization using generally the same conditions that have been used in the past with slurries of catalyst.
  • the invention is particularly useful for the homopolymerization or copolymerization of mono-1-olefins. Olefins having 2 to 18 carbon atoms would most often be used.
  • the invention is considered particularly applicable to slurry or particle form polymerization processes, especially continuous polymerization processes such as disclosed in U.S. Pat. Nos. 3,152,872 and 4,424,341, the disclosures of which are incorporated herein by reference.
  • the fumed silicas which were obtained from Cabot Corporation were either used as supplied or dried in the oven overnight.
  • the aluminum oxide and titanium dioxide were obtained from Degussa.
  • the samples were shaken to mix the additive and the catalyst thoroughly and then allowed to settle.
  • the initial evaluations were done by tipping flasks containing the resulting mixture and comparing the angle of repose of the solids.
  • the fumed refractory oxides were all found to provide improvements in catalyst flow.
  • the larger particle size Grade G alumina flowed poorly. At levels similar to those used for HS-5, i.e. 5 g alumina/20 g catalyst, no flow improvement was demonstrated.
  • At larger amounts, i.e. 50 g alumina/20 g catalyst only a very slight improvement, if any, was noted.
  • Catalyst A contained about 10 weight percent prepolymer.
  • Catalyst B was a commercial catalyst containing prepolymer.
  • Catalyst C was a catalyst which had been treated with diethylaluminum chloride after the titanium tetrachloride treatment, Catalyst C contained about 40 weight percent prepolymer.
  • Catalyst D also contained prepolymer.
  • a slurry of the catalyst was well shaken and mixed with varying amounts of the refractory oxide and when employed, antistatic agent in a liquid diluent.
  • the antistatic agent Stadis 450 was obtained from DuPont. From the solid weight percent of the original catalyst slurry, determination of the weight percentage of refractory oxide based on a total solid weight was possible.
  • the polymerizations were carried out at 90° C. in a 3.8 liter autoclave reactor. The reactor was prepared for polymerization by heating to 110° C. for one hour. The reactor was then cooled to room temperature where it was flushed with nitrogen free isobutane.
  • the melt index (MI) and high load melt index (HLMI) were measured using ASTM-1238 conditions of 190/2.16 and 190/21.6 respectively.
  • Bulk densities of the polymer were measured by weighing a 100 ml graduated cylinder in which the polymer fluff had been lightly tapped.
  • Polymer densities were determined according to ASTM-D-1505 using compression molded discs of polymer. Corrected polymer densities were obtained by normalizing the polymer densities for a MI value of one. Titanium and chloride content of the polymer and the solution above the catalyst were determined by X-ray fluorescence. The results of the various polymerizations are summarized in Table 2.
  • runs 2 and 6 respectively represent control polymerizations using comonomer and no refractory oxide. It will be noted that runs 1 and 3 were polymerizations which did not employ the introduction of hexene comonomer.
  • a comparison of runs 2 and 5 shows that the fumed silica M-5 caused no significant change in the titanium and chloride levels.
  • the comparison of runs 6 with runs 8-11 shows that the fumed silica HS-5 did not result in any significant change in the titanium or chloride levels.
  • the data also shows that the addition of the fumed oxides and/or the antistatic agent did not have an adverse effect on either comonomer incorporation, catalyst activity, or polymer bulk density. This is in contrast to observations that have been made in the past when the polymerizations were conducted in the presence of the larger particle size high surface area silica such as Davidson Grade 952 silica gel.
  • Other work with titanium catalysts has demonstrated that even when Cab-O-Sil HS-5 fumed silica is used at a silica to catalyst weight ratio of 0.175/1, the polymer properties were essentially equivalent, within the scope of experimental error, to those obtained using the catalyst without the fumed silica.
  • Example III Using the same technique as described in Example III, the effect of three other silicas on the flow rate of the catalyst slurry were evaluated.
  • the three silicas evaluated were larger primary particle size silicas, namely Sylox® 2, Syloid® 63, and Syloid® 244. Those silicas had average primary particle sizes of 2 to 3 microns, 9 microns, and 3 microns respectively.
  • the Sylox® 2 provided a better flow rate than the Syloid® 244 or Syloid® 63; however, that flow rate was not nearly as good as the flow rate obtained with the same weight percent of Cab-O-Sil HS-5.
  • the Cab-O-Sil HS-5 provided a superior flow rate to the larger primary particle size silicas.
  • One of the particulate chromium-containing catalysts that has been used in the past is prepared by treating a porous silica such as Davidson 952 grade silica with chromium.
  • a porous silica such as Davidson 952 grade silica
  • a number of runs were carried out using a procedure like that described in Example III.

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Polymerization Catalysts (AREA)
  • Polymerisation Methods In General (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
  • Graft Or Block Polymers (AREA)
US07/883,602 1992-05-15 1992-05-15 Olefin polymerization Expired - Fee Related US5179178A (en)

Priority Applications (17)

Application Number Priority Date Filing Date Title
US07/883,602 US5179178A (en) 1992-05-15 1992-05-15 Olefin polymerization
CA002093461A CA2093461C (en) 1992-05-15 1993-04-06 Olefin polymerization
AU36745/93A AU651273B2 (en) 1992-05-15 1993-04-06 Process for polymerizing olefins
ZA932856A ZA932856B (en) 1992-05-15 1993-04-22 Process for polymerizing olefins
KR1019930008053A KR100278081B1 (ko) 1992-05-15 1993-05-11 올레핀 중합 방법
JP11069493A JP3268884B2 (ja) 1992-05-15 1993-05-12 オレフィンの重合方法
MX9302763A MX9302763A (es) 1992-05-15 1993-05-12 Proceso para la polimerizacion de olefinas.
HU9301392A HU211449B (en) 1992-05-15 1993-05-13 Process for producing catalyst slurry with improved flow characteristic and for polymerization of olefins
NO931749A NO300694B1 (no) 1992-05-15 1993-05-13 Olefinpolymerisering
DE69306852T DE69306852T2 (de) 1992-05-15 1993-05-14 Olefinpolymerisation
YU33293A YU48361B (sh) 1992-05-15 1993-05-14 Postupak za polimerizaciju olefina
AT93107880T ATE146802T1 (de) 1992-05-15 1993-05-14 Olefinpolymerisation
EP93107880A EP0570000B1 (en) 1992-05-15 1993-05-14 Olefin polymerization
DK93107880.2T DK0570000T3 (da) 1992-05-15 1993-05-14 Olefinpolymerisation
ES93107880T ES2096138T3 (es) 1992-05-15 1993-05-14 Polimerizacion de olefinas.
SG1996005323A SG43200A1 (en) 1992-05-15 1993-05-14 Olefin polymerization
GR960403669T GR3022341T3 (en) 1992-05-15 1997-01-22 Olefin polymerization

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Application Number Priority Date Filing Date Title
US07/883,602 US5179178A (en) 1992-05-15 1992-05-15 Olefin polymerization

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US (1) US5179178A (sh)
EP (1) EP0570000B1 (sh)
JP (1) JP3268884B2 (sh)
KR (1) KR100278081B1 (sh)
AT (1) ATE146802T1 (sh)
AU (1) AU651273B2 (sh)
CA (1) CA2093461C (sh)
DE (1) DE69306852T2 (sh)
DK (1) DK0570000T3 (sh)
ES (1) ES2096138T3 (sh)
GR (1) GR3022341T3 (sh)
HU (1) HU211449B (sh)
MX (1) MX9302763A (sh)
NO (1) NO300694B1 (sh)
SG (1) SG43200A1 (sh)
YU (1) YU48361B (sh)
ZA (1) ZA932856B (sh)

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0690878A1 (en) * 1993-03-25 1996-01-10 Mobil Oil Corporation Process for forming a granular resin
US20050239641A1 (en) * 2004-04-22 2005-10-27 Mcdaniel Max P Methods of preparing active chromium/alumina catalysts via treatment with sulfate
US20050239977A1 (en) * 2004-04-22 2005-10-27 Mcdaniel Max P Polymers having low levels of long chain branching and methods of making the same
US20060155082A1 (en) * 2005-01-10 2006-07-13 Mcdaniel Max P Process for producing polymers
US20080287287A1 (en) * 2007-05-16 2008-11-20 Chevron Phillips Chemical Company Lp Methods of preparing a polymerization catalyst
EP2374537A2 (en) 2004-04-22 2011-10-12 Chevron Phillips Chemical Company LP Methods of preparing active chromium/alumina catalysts via treatment with sulfate and polymers produced using the chromium/alumina catalysts
US20130018158A1 (en) * 2007-11-30 2013-01-17 Borealis Technology Oy Catalyst with low surface area
US8399580B2 (en) 2010-08-11 2013-03-19 Chevron Philips Chemical Company Lp Additives to chromium catalyst mix tank
US8440772B2 (en) 2011-04-28 2013-05-14 Chevron Phillips Chemical Company Lp Methods for terminating olefin polymerizations
WO2013096106A1 (en) 2011-12-19 2013-06-27 Chevron Phillips Chemical Company Lp Use of hydrogen and an organozinc compound for polymerization and polymer property control
US8487053B2 (en) 2011-11-30 2013-07-16 Chevron Phillips Chemical Company Lp Methods for removing polymer skins from reactor walls
WO2014035875A1 (en) 2012-08-27 2014-03-06 Chevron Phillips Chemical Company Lp Vapor phase preparation of fluorided solid oxides
US8673806B2 (en) 2009-01-29 2014-03-18 W.R. Grace & Co.-Conn. Catalyst on silica clad alumina support
US8703883B2 (en) 2012-02-20 2014-04-22 Chevron Phillips Chemical Company Lp Systems and methods for real-time catalyst particle size control in a polymerization reactor
US8940842B2 (en) 2012-09-24 2015-01-27 Chevron Phillips Chemical Company Lp Methods for controlling dual catalyst olefin polymerizations
WO2016085856A1 (en) * 2014-11-24 2016-06-02 Univation Technologies, Llc Composition comprising particles
US9365664B2 (en) 2009-01-29 2016-06-14 W. R. Grace & Co. -Conn. Catalyst on silica clad alumina support
WO2016196490A1 (en) 2015-06-01 2016-12-08 Chevron Phillips Chemical Company Lp Liquid-solid sampling system for a loop slurry reactor
WO2017213832A1 (en) 2016-06-09 2017-12-14 Chevron Phillips Chemical Company Lp Methods for increasing polymer production rates with halogenated hydrocarbon compounds
US10266618B2 (en) 2014-11-24 2019-04-23 Univation Technologies, Llc Chromium-based catalyst compositions for olefin polymerization
US10273315B2 (en) 2012-06-20 2019-04-30 Chevron Phillips Chemical Company Lp Methods for terminating olefin polymerizations
US11466104B1 (en) 2022-02-01 2022-10-11 Chevron Phillips Chemical Company Lp Ethylene polymerization processes and reactor systems for the production of multimodal polymers using combinations of a loop reactor and a fluidized bed reactor
WO2023114643A1 (en) 2021-12-15 2023-06-22 Chevron Phillips Chemical Company Lp Production of polyethylene and ethylene oligomers from ethanol and the use of biomass and waste streams as feedstocks to produce the ethanol
WO2023205575A1 (en) 2022-04-19 2023-10-26 Chevron Phillips Chemical Company Lp Loop slurry periodogram control to prevent reactor fouling and reactor shutdowns

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2000050466A1 (en) 1999-02-22 2000-08-31 Borealis Technology Oy Olefin polymerisation process
CN106687236B (zh) 2014-09-19 2019-05-14 Ntn株式会社 滑动部件及其制造方法

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Kirk Othmer Encyclopedia of Chemical Technology, vol. 20, Third Edition, pp. 766 776. *
Kirk-Othmer Encyclopedia of Chemical Technology, vol. 20, Third Edition, pp. 766-776.

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US20050239641A1 (en) * 2004-04-22 2005-10-27 Mcdaniel Max P Methods of preparing active chromium/alumina catalysts via treatment with sulfate
US20050239977A1 (en) * 2004-04-22 2005-10-27 Mcdaniel Max P Polymers having low levels of long chain branching and methods of making the same
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US7214642B2 (en) 2004-04-22 2007-05-08 Chevron Phillips Chemical Company Lp Methods of preparing active chromium/alumina catalysts via treatment with sulfate
US20060155082A1 (en) * 2005-01-10 2006-07-13 Mcdaniel Max P Process for producing polymers
US20090124768A1 (en) * 2005-01-10 2009-05-14 Mcdaniel Max P Process for producing polymers
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Also Published As

Publication number Publication date
JPH0632812A (ja) 1994-02-08
SG43200A1 (en) 1997-10-17
ZA932856B (en) 1993-11-23
EP0570000B1 (en) 1996-12-27
NO931749D0 (no) 1993-05-13
NO300694B1 (no) 1997-07-07
AU3674593A (en) 1993-11-18
HU9301392D0 (en) 1993-09-28
DE69306852D1 (de) 1997-02-06
ATE146802T1 (de) 1997-01-15
EP0570000A1 (en) 1993-11-18
MX9302763A (es) 1993-11-01
CA2093461C (en) 1997-02-04
NO931749L (no) 1993-11-16
DE69306852T2 (de) 1997-05-07
HU211449B (en) 1995-11-28
YU48361B (sh) 1998-07-10
JP3268884B2 (ja) 2002-03-25
ES2096138T3 (es) 1997-03-01
KR930023380A (ko) 1993-12-18
DK0570000T3 (da) 1997-01-20
AU651273B2 (en) 1994-07-14
HUT66366A (en) 1994-11-28
KR100278081B1 (ko) 2001-01-15
YU33293A (sh) 1996-02-19
GR3022341T3 (en) 1997-04-30
CA2093461A1 (en) 1993-11-16

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